Process and apparatus for treating mineral oils



Dec. 13, 1938. M. R. FENSKE ET AL PROCESS AND APPARATUS FOR TREATING MINERAL OILS 5 Sheets-Sheet 1' Filed July 13, 1934 Dec. 13, 1938. M R, FENSKE ET AL 2,139,943

PROCESS AND APPARATUS FOR TREATING MINERAL OILS Filed July 13, 1954 3 Sheets-Sheet 2 I a e7 %.2. J9 gm 38 I g j/ Dec. 13, 1938. R FENSKE ET AL 2,139,943

PROCESS AND APPARATUS FOR TREATING MINERAL OILS Filed July 13, 1934 5 Sheets-Sheet 3 WAV/ PatentedDec. 13, 1938 a UNITED srAr-es PATENT orrics PROCESS AND armmrosxroarmmrmo MINERAL oms i MerrellR. Fenske and 'WiIbertZB. McCluenState College, Pa., assignors :to .Pennsy'lvariia fPetro- 'leum Research Corporation, "a "corporation of Pennsylvania Application July .13, 1934, SeriallNo. 135,026 -12 Claims. (o1. 196- 13) This invention pertains generally to thepurivAny of thebatch methodscustomary in solvent fication of mineral'oils, and pertains particularly extractionmay beresorted to,in which case,the to the extraction from crude petroleum or'prodadsorbent materia1 .is added to the batch in a ucts thereof of materials considered deleterious, .manner similartotthat-employed incont'act filby thesimultaneous use of a selectivexsolvent 'tration. After suitable agitation of the"oil,'soland an adsorbent material. vent, andadsorbent.material, the .solid maybe Various means are employed for the removal I filtered out, whereupon the'liquid will vform-into from crude petroleum or fractions thereof of .atwo-layersystem andthe'layers maybe sepaundesired substances. .The substances to be re- .ratedbydecantation, orotherwise.

1o moved depend generally'upon the source-of the :It :is preferred, however, to-employ asystem crude and/or the character'of the prior treatsimilar to the continuous countercurrent sysment thereof. These materials include asphaltic tems employed in solvent :extraction in which substances, resins, nitrogen compounds, sulphur casethe filtration-is analogous'to percolation.

compounds, oxygen-containing compounds, un- By extracting andfiltering simultaneously and l5 saturated materials, naphthenic acids, color in the same sphere of action, a decidedly sharper .15 bodies, etc. I separation between desired and undesired mate- "In the prior art, there are 'two recognized rials may be-obtain'ed. Furthermore, the useful methods employed for thegpurpose ofextracting life of the adsorbent material may be greatly these materials. One of these methods involves extended, and the necessity for revivification extracting the crude petroleum or fraction theremade much less frequent. 20 of with a suitable solvent, and the other involves 'Anyof the batch, multiple batch, batch counfiltration through a suitable adsorbent material tercurrent, continuous countercurrent, or other such as fullers earth, silica gel, bauxite, activated systems for obtaining -..contact between solvent charcoal, Florida earth, etc. and oil insolventextraction processes may be In solvent extraction processes, considerable adapted to the .invention, provisionbeing .made ,25 diificulty is encountered in obtaining a :clean in each case for obtaining proper contact be- ,separation between desired and undesired m'atetween :solvent and *oil, :adsorbent material and rials, making it necessary to extract from the Oihandsolventand adsorbent material. original oil larger quantities than would be :Continuous countercurrent systems, and'parnecessary if a sharp separation could be ob- Iticularlythose in whichthe countercurrentfioweo tained. .In other words, the extract or :material is obtainedbyadiiference.in density betweenthe of lesser value contains 'constituents which, if Solvent and oil, are very suitable. The. apparatus separated from the extract, would have a quality employed in'thesesystems, in many cases, takes comparable to that of the original oil it not of the the general shapeofa tower. In these cases, the

raffinate. adsorbent material'maybeplaced in thetower in Furthermore, solvents are unable to extract :a manner similar 'to packing. For themost efficertain substances from lubricating oils which cientoperation,careshould'be exercised to avoid appear to be soluble in the solvents. This is substantial channeling. Channeling throughadapparently due to the inefficiency of the processsorbent materialis. generallyassociated"with in- 40 ing method or the incomplete utilization of the creased pressure, resulting from the desire to .40

solvent in prior art methods of treatment. increase the rate dffiow.

Filtration through adsorbent material is large- Apparatus .adapted to permit a high rate'of ly used for removing color bodies and othersimifiow'Without channeling is illustrated in the .lar undesiredconstituents from the oil. As a drawings'in which rule, largequantities of adsorbent material are Fig.'1.is an elevation of .a column adapted for 45 required. Furthermore, the adsorbent material carrying outtheprocess;

must be repeatedly revivifled,and eventually its FiguresZA and2B comprise a sectional elevaadsorbent characteristics entirely disappear. tlonof the column shown in'Fig. 1, Fig. 2Aillus- The invention herein is based upon the distrating the upper portionandFig. 2B the lower .30 covery that sharper separation between desired portion; 5i)

and undesired constituents may be obtained by Fig. 3 isa sectiononline 3-3 of'Fig. 1; extracting the oil with a suitable solvent in the Fig.4 is a viewjtaken nline 4- 4 of Fig. 1; and presence of an adsorbent material, or, in "other Figures-5A and 53 comprise a sectional elevawords, by extracting in the presence Of a filter tion-of a modified form'of column. 55 medium. Referring now'more particularly to Figures 1 .55

to 4 of the drawings in which a detailed construction is shown for the purposes of illustration, In is a column comprising a vertically arranged main portion H, a lower feeding and segregating chamber l2, an upper segregating chamber [3, and an upper feeding chamber l4.

1 Main portion H may be of any suitable construction, and preferably presents a path to the countercurrently flowing oil and solvent which is of a character that will bring the oil and solvent into intimate contact of a very large surface area compared'to their volumes. This is accomplished by employing adsorbent material, pref-- erably in granular form, as packing. The construction of column H is. also preferably such that a substantial degree of channeling cannot take place. This is accomplished by causing the counterflow of solvent and oil to take place through a path or a plurality of paths of relatively small diameter with the adsorbent material arranged in the path or paths as a contact medium.-

To obtain these results, shell l6 of main portion H is provided with tube sheets I! and I8 at its ends. Tube sheets I! and I8 have aligned apertures which receive and support the opposite ends of a plurality of spaced tubes I9.

Shell I6 is shown with apertures 20 at its top and apertures 2| at its bottom. These apertures are shown with tubular extensions 22 and 23 respectively to facilitate connection with any suitable means for circulating, heating, or cooling fluids over and about the outsides of tubes [9 for temperature control purposes.

Tubes H! are packed with a suitable adsorbent material 24 preferably in granular form, the granules being of any desired size. The adsorbent material may be supported in the tubes by any suitable means, for instance, by plate 25 held between flanges 28 at the bottom of column l0, said plate being reticulated opposite tubes l9 and supporting a strip of fabric 25A, of finer mesh than the adsorbent material. Any other construction may be substituted.

Tubes l9 may be of any desired number, that is, one or more. The number employed will be governed by the desired through-put of the column.

The tubes l9 may have a cross section of any desired geometrical configuration and withincertain limits of any desired area. The cross section of each tube I9 is preferably limited to an area sufllciently small to prevent serious channeling after the adsorbent material has been arranged therein."

The preferred limiting cross sectional area for each tube l9 will be not only a function of the type and mesh of adsorbent material employed, but also of the manner in which the adsorbent material is arranged in each tube, for instance, of the degree of uniformity of distribution. Since the tubes l9 may have sides which are straight or indented or which are of any other surface configuration, the departure of a tube from a straight or continuous form will have its influence. For this reason a definite limit in cross sectional area, which, if exceeded in size will no longer demonstrate the substantial increase in efiiciency which we have discovered results from a constriction of cross sectional area, cannot be given, but may be readily determined,

' for instance, by testing the efficiency of single should proceed with caution after exceeding a cross sectional area equivalent to that of a circular tube in the neighborhood of three inches in diameter although, with'the proper selection of adsorbent material and a careful distribution in each tube, it is possible that largercross sectional areas may be employed while in other cases smaller cross sectional areas may be required.

Therefore, the term "relatively small cross sectional area or its equivalent, when employed in this specification and in the claims is intended to mean a cross section which, when taken in conjunction with the specific adsorbent material employed, is sufliciently small to materially increase the contacting efiiciency because of the constriction of its area.

Whether or not channeling will become an important factor will also depend somewhat upon the pressure differential and the physical state of the adsorbent material.

Although a large diameter tube is likely to be less efficient, it may, nevertheless, be employed, for the invention in its broadest aspects includes not only any tower or column, regardless of diameter or type, but also any type of contacting apparatus.

The lower feeding and segregating chamber I2 is attached to the main portion II by flanges 28 and freely communicates with the tubes I 9 through the reticulations in plate 25 and fabric 25A. Chamber I2 has a tubular extension 29 at its bottom for the egress of the heavier solution and a tubular extension 30 in its side for ingress of the lighter liquid. A sight gage 3| may be provided to show the height of the heavier liquid in chamber I2 or extension 29 as the case may be.

segregating chamber I3 is attached to the upper end of main portion 1 I by flanges 33. To prevent the adsorbent material from being carried up into chamber l3, a plate 32 secured between flanges 33 may be provided to secure a layer of fabric 32A over the upper ends of tubes l9, the plate 32 being reticular opposite the ends of the tubes. Any other construction may be substituted.

Chamber l3 has a tubular extension 34 at its side for the egress of lighter solution.

Upper feeding chamber I4 is disposed above chamber 13 and is secured thereto by flanges35.

The disc-like plate 36 is disposed between chambers l4 and I3. Plate 36 has a plurality of feeding tubes 31. There is one tube 31 for each tube I9. Each tube 31 extends downward through chamber l3 and into a tube IQ for at least a short distance.

Chamber M has a tubular extension 38 at its top for the ingress of heavier liquid and a sight gage 39 to show the head on the heavier liquid.

Any suitable remotely registering gage may be substituted for sight gage 3| or for sight gage .39 or both particularly if all of the instruments are to be mounted on a single instrument board.

In operation, the heavier liquid (either solvent or oil as the case may be) is fed into chamber ll through extension 38 and is preferably maintained therein at a suitable level. The lighter liquid (either oil or solvent as the case may be) is fed into chamber l2 throughextension 30. The heavier liquid flows downwardly through tubes 31 into tubes l9. Any suitable metering means may be provided so that the feeding of heavier liquid will be uniform. For instance, tubes 31 might be of equal length and equal inner diameter.

Similar metering orifices might be provided for feeding the lighter liquid by substituting a construction similar to that of chambers I3 and M for chamber l2. However, it is found that the lighter liquid will be fed uniformly up into tubes I9 since the lighter liquid will enter each tube l9 at the same pressure.

The two liquids pass each other in tubes l9 due to the difference in density and intimately contact each other in so doing, whereby the oil is extracted by the solvent. At the same time, the oil intimately contacts the adsorbent material, whereby the oil is filtered. The solvent intimately contacts the adsorbent material whereby a very large part of those materials which are adsorbed from the oil are dissolved in the solvent. The adsorbent material is thus continuously revivified.

As a result of the foregoing, two immiscible solutions of different density are formed, the lighter of which collects in chamber l3 and the heavier of which collects in chamber l2.

The lighter solution may be continuously withdrawn through extension 34, and the heavier solution may be continuously Withdrawn through extension 29.

A two-layer system is preferably maintained in chamber I2 or extension 29 to assure the upward flow of the lighter liquid. Valve 42 and gage 3| Will assist in maintaining the two-layer system.

It will be noted that in the construction shown the solvent and oil flow countercurrently to each other in a plurality of separate streams of substantially equal size, the streams of each liquid flowing through separate paths of relatively small diameter, with an adsorbent material disposed preferably substantially uniformly throughout said paths. By this means channeling of any one stream through its associated countercurrently flowing stream is substantially prevented and the two countercurrently flowing liquids are caused to spread out into thin films over and about the adsorbent material thus presenting not only a very large surface area to each other but also to the adsorbent material.

Since the result of having tubes 19 of'substantially the same size and of substantially equally dividing each feed liquid'among the tubes 19 is to maintain substantially the same proportion of solvent phase to oil phase in each tube, it will be obvious that tubes l9 may be of different s zes and that the feeding rates may vary accordingly, especially if substantially the same proportion of phases is maintained in each tube.

In other words, the result of having tubes 19 of the same size and of maintaining uniform feeding conditions for each tube, is to cause the raffinate phase produced by each tube to be of substantially the same composition as the raflinate phase produced by any other tube; and to cause the extract phase produced by each tube to be of substantially the same composition as the extract phase produced by any other tube. From this it will be obvious that if tubes l9 should vary in size the feeding rates may be adjusted to obtain similar conditions.

However, improved results may be obtained to a certain degree even though ideal conditions are not approached.

Should difficulty be experienced with flooding of the column, the rate of feed of'oil and/or 501- vent may be reduced. and/or the viscosity of the 1 oil might be reduced either by raising the temperature of extraction or by the previous mixing with the oil of a quantity of the solvent up to that amount which normally goes into solution therewith. The tendency to flood might also be diminished by modifying the granular character of the adsorbent material so as to afford more free space.

The column may have any desired height, that is, thetubes l9 may be of any desired length.

For instance, the tubes l9 might be 30 feet in length and might be packed with to 30 mesh fullers earth; or, if a number of columns are to be connected in series, obviously the tubes l9 may be of shorter length sincethe effective length of the combination will be the sum of the lengths of the tubes IQ of all of the columns.

If the solvent is selective as to type of molecule, and depending, of course, upon the particular solvent employed. the order in which the various classes of hydrocarbon molecules will be dissolved by the solvent will generally be unsaturated, aromatic, naphthene, paraifin. By striking coincidence, this is the same order in which the various classes of hydrocarbons are adsorbed. The result is that as the oil proceedsthrough thecolumn, it gives up these materials in substantially the order named to boththe solvent and to the adsorbent material but probably not with the same ease or degree with respect to any class of compounds or individual compounds of the class. Therefore, certain compounds which are not readily adsorbed may be dissolved out by solvent, and other compounds whieh are not readily dissolved out directly by solvent may be adsorbed, and then (Whether with or without a change in molecular structure), dissolved by solvent. Other materials will be dissolved either directly or after being adsorbed depending upon the distribution ratio.

For any one extraction temperature, the solvent to oil ratio and the rate of flow is so adjusted that the desired yield and quality'of raffinate is obtained.

Conversely, when considering the solution of adsorbed materials in the solvent, the adsorbent material may be considered as moving relatively countercurrently to the solvent.

The efllciencies of countercurrent systems are,

therefore, made possible in the use of this invention.

Many solvents which are selective as to type of molecule and therefore suitable for solvent extraction purposes are also suitable for maintaining the adsorbent medium substantially revivified. Among these solvents are methyl alcohol, ethyl alcohol, isopropyl alcohol, acetone, liquid sulfur dioxide, ethyl acetate, and the ethylene glycol ethers and their acyl derivatives.

Other solvents selective as to type of molecule are phenol, benzonitrile, aniline, methyl acetate, cresylic acid, pyridine, phenyl acetate, benzaldehyde, propionaldehyde, allyl alcohol, furfural, nitrotoluene, mononitronaphthalene, furfuryl alcohol, beta beta dichlorethyl ether, cresol, crotonaldehyde, acrolein, acetaldehyde, aniline 'oil, estersol, ethylene chlorohydrin, nitrobenzene, tetrahydrofurfuryl alcohol, mixed toluidincs, orthotoluidine, xylidine, polyhydric alcohols, tricresyl phosphate, tolyl formate, methyl thiocyanate, al

lyl isothiocyanate, phenyl thiocyanate, tolualde-' hyde, etc. l

Should a solvent not possess the desired revivification properties,-such properties might be imparted by adding to the solvent, for instance, to or more of ethyl alcohol, methyl alcohol or acetone; or a suitable quantity of an organic acid such as acetic acid or even an inorganic acid such as hydrochloric acid or sulfuric acid in relatively small amounts, might be added to the solvent, particularly if the acid and solvent do not react chemically. b

When batch methods are employed, the adsorbent material may be added to the oil at the same time that the solvent is added to the oil or before or after.

By decreasing the extraction temperature in the direction of solvent fiow in a countercurrent system and by suitable adjustment of the various temperatures, the solvent may be brought to a supersaturated condition before leaving the column, which results in a selective precipitation of a part of the dissolved hydrocarbons in the inverse order of their solubility. These precipitated materials flow through the column along with the oil and are redissolved in the order of their solubility in the solvent, only to be reprecipitated in the inverse order of their solubility.- The most soluble hydrocarbons are carried ofi with the solvent as extract, and the least soluble are carried off with the oil as raffinate.

A similar rectifying efiect can be obtained by the introduction into the column, that is into the tubes l9 at one or more points intermediate their ends, of a substance or-substanceswhich tend to decrease the solubility of theoil in the solvent (such as another solvent of lower solubility for the oil). Upon the introduction of such substance or substances at a point or in graduated amounts at a plurality of points along the path of solvent .flow, hydrocarbons may be selectively precipitated only to be redissolved and reprecipitated in the manner above pointed out.

This same rectifying effect maybe obtained by decreasing the solvent-oil ratio along the column, for instance, by diverting the solvent stream, vaporizing a part of the solvent and returning the depleted solvent stream and precipitate to the column. If a plurality of columns are joined in series, the vaporization might take place between columns, in which case the precipitate would be 7 returned to the preceding column and the solvent stream would continue on to the subsequent column. I

Column I0 might also be employed for purely precipitation purposes. For instance, a solution of solvent and oil might be flowed through column in and by reducing the solvent power of the solvent in the direction of solvent flow such as by reducing the temperature, introducing a substance or substances and/or vaporizing a part of the solvent, oil components may be precipitated in the-inverse order of their solubility. The precipitate may be caused to' flow countercur'rently to the solution by choosing a suitable point of feed for the solution.

For instance, if the precipitate is heavier than the solution, the solution may be fed into the column at 30 and may leave the column at 34. In this case, the precipitate would flow downwardly through thecolumn, collect in chamber l2 and would be removed through valve 42. On the other hand, if the precipitate is lighter than the solution, the solutionmay be fed into the column through chamber I4 and removed through valve 42. In this case, the precipitate would rise, through. the column, collect in chamber I3 and would be removed through 84.

Rectification-of the precipitate results from its flowing counter-currently to the solution, since any more solubleigcomponents will be substituted in the solution for less soluble components, the

latter being precipitated. This rectifying action may be increased by having the solution enter the column in an unsaturated state, since in this case, solution offmore soluble components may take place other than and in addition to solution by substitution.

A saturated solution may be brought to an unsaturated state by raising the temperature, by adding more solvent, and/or by removing substances which tend to reduce the solubility of hydrocarbons in the solvent.

Column in may also be adapted to certain extraction processes wherein a counterflow of solvents is effected, and in which the oil is introduced into the counterflow. In this case, the heavier solvent would be fed into the column through chamber M, the lighter solvent through the chamber I2, and the oil would be metered into tubes l9 at a suitable point or pointsintermediate the ends thereof by any suitable means such as metering orifices.

The feedingof solvent and/or oil might take place at a plurality of points along the column. Various other modifications are possible. While the invention has been particularly 'de scribed in connection with the treatment of liquid oil, it is to be understood that it may be employed for the treatment of other materials whether in the liquid, solid, or vapor phase at normal temperatures and. pressures. For instance, par'affin .wax may be purified by flowing the'wax in melted form through the column countercurrently to a wax purifying solvent such as ethylene dichloride or methyl ethyl ketone,both of which have a relatively low solvent power for paraflin wax, but have a relatively high solvent power for entrained'oil.

Increased pressures may be employed to maintain the solvents wholly or partially in the liquid phase as desired. I

Should the adsorbent packing material become exhausted or should it be desired to revivifyfthe same, it is merely necessary to remove it from the column and to replace it with new or revivified adsorbent material.

It is, of course, possible to provide a construction whereby the adsorbent material may be caused to move slowly through the column and thus be continuously replaced by new or revivified adsorbent material.

A construction suitable for this purpose is illustrated in Figures 5A and 53 wherein column 50 takes the general form of column ID of Figures 2A and 2B. In column 50, main portion l I of column in description.

In Figure 5A, chambers l3 and [4 of Figure ZA have been substituted by chambers 5i 52, and 53. Chamber 5| is the segregating chamber for light solution and differs from chamber 13 in that tubular filters 54 (which may be of any suitable construction) join tubes I9 with chamber 52.

Chamber 52 is for the feeding of adsorbent material into the tops of the tubular filters 54 through which the. adsorbent material is con ducted into thetubes I9.

Chamber. 53 may be in all respects similar to chamber Hi. The disc-like plate 55, between chambers 52 and 53 has a plurality of apertures ID has been duplicated for purposes of simpilicity ends' of tubes 56 to prevent clogging by adsorbent material. v

In Figure 5B, chamber 12 of Figure 2B is substituted by chamber59. Chamber 59 vdiifers from chamber l2 chiefly in that tubular filters 60 extend from the lower ends of tubes. 19 entirely through chamber 59, each tube 60 connecting with an individual adsorbent materialflow-regulator 61 illustrated as a tubular casing (i2 housing a screw 63. Shaft 64 ofeach screvv'liiiv is illustrated as extending down through the bottomof areceiver 65, and for the purposes of assuring uniform conditions in each tube 49, shafts 64 may be uniformly driven as illustrated diagrammatically at 66. q i

In the operation of column 50, the solventand oil and light and heavy solutions flow "in and out of the column "in in column l6.

The essential difierences are that the light solution disengages itself from the adsorbent material in chamber 5| bypassing through tubular filters 54, the heavy solution .disengages itself from the adsorbent material in chamber .59 by passing through tubular filters 60, andthe solvent or oil, whichever is thelighter, enters the bottoms of tubes l9 by first passing inwardly through tubular filters '60.

Screws 63 may be operated at any-desired rate, for instance,at a rate just suilicient'to maintain the adsorbent material in tubes l8 in'a suitably active condition. The operation may-be intermittent or constant as .desired. The'screws 63 preferably comprise a plurality of turns of small pitch and preferably fit closely in their housings so as to prevent an inordinate amount of seepage into receiver 65. 1

Any other construction may-be substitutedfor the screws 63, or a construction mightbe adopted which would cause the adsorbent material 'to ascend through tubes l9 rather than descent therethrough. a

For instance, it might be desired to have the adsorbent material flow countercurrently to the oil also when the oil is heavier than the solvent.

However, to cause adsorbent material to flow through the column, a special construction such as that of Figures 5A and 5B is not essential, .since a slurry of adsorbent material and solvent, orof adsorbent material and oil might be made and might be fed through the column l0 countercurrently to the other liquid, for instance, byfeeding into column 1'0 through chamber l4 and modifying tubes 3'! to take care of the desired rate of flow. Separation of spent slurryfrom the other liquid might take place in the usual manner by layer formation, whereupon the slurry might be separated into its constituents.

The term solvent in its broader phases includes any compound or compounds whether in the vapor, liquid and/0r solid phase and regardless of its influence upon the base material.

Having particularly described the invention, it is to be understood that changes, omissions, additions, substitutions'and/or modifications other than those specifically mentioned may be made without departing from the spirit of theinvention. I'he claims, therefore, are intended to be limited only as required by theprior art.

For instance the solvent and oil might :be mixed the same manner asthey do mechanically and then flowed in one direction through the tower, or, for instance, through any of the filters used iorpercolating oil through adsorbent "material. mechanical mixtures makes feeding diflicult or unsatisfactory the temperature of the oil and solvent might be raised so as to form a solution of same. This might be followed by cooling for instance in the tower or filter so as to permit the, desired formation of phases.

Reference is made to applicants copending applications Serial No. 688,416 filed September 6, 1933, Serial No. 699,050 filed November 21,1933, Serial No. 697,344 "filed November 9, .1933, Serial .No. 697,858 filed November 13, 1,933, and Serial No. 10,932 filed March 113. .1935.

We claim;

1. A process 'for purifying a mineral .011 comprising flowing ;said mineral oil in aplurality of segregatedstreams of substantially equal size and If formation layers in the of relatively small cross sectional area counter- .currentlyto a like number of similarstreams of a suitable solvent, each segregated stream of oil contacting a segregated stream of solvent in a separate path containing an adsorbent material.

2.. A. process :for purifying va lubricating oil comprising flowing said lubricating oil in a plu-' rality of segregated streams-of substantiallyequal size and of relatively small'cross sectional area countercurrently to a like number of similar streams of suitable solvent, each segregated stream of oil contacting a segregated stream of solvent in a separate path containing an adsorbentmaterial.

:3. A process for purifyin a lubricating 011 comprising flowing said .oil through a column countercurrently to a .suitablesolvent under convditions causing the formation of two liquid phases, .andflowing adsorbent material through said columncountercurrently .to .said oil, said adsorbent material :being present in said column in sufficient uantity 'to function as a contact medium between said. solvent and oil.

4. Apparatus comprising. ,a column, means 8-18- sociated with said column for. causing a mineral :oil andasolyent to flow .countercur-ren-tly there- ;through, means :Eor dividing each liquid into a plurality of streams .of substantially equal size, a plurality of segregated paths, an adsorbent material in each path, means for contacting each the other liquid in .a separate path of said sege regated paths, means for feeding adsorbent mav,terial into said column, and means for causing said adsorbent material -:to :fiow through said paths.

6. Apparatus comprising, ,a column, means .associated with said column .-for causing a mineral .oil and a solvent to flow countercurrently therethrough, means .for dividing :each liquid into a plurality of streams .of substantially .equal size, ,a plurality of segregatedpaths, an adsorbent ,maiterial in :each' path, means for contacting each stream of each liquid with .a separate streamer the other liquid in a:-separ,ate, ;path, means for .stream of each liquid with a separate stream of feeding adsorbent material into said column, and means for causing said adsorbent material to flow through said paths countercurrently to said oil.

'7. Apparatus comprising, a column, means associated with said column for causing liquid phases to flow countercurrently therethrough by virtue of a difference in density such as in the solvent treatment of petroleum products, means for dividing each phase into a plurality of streams, a plurality of segregated paths, an adsorbent material in each path, and means for contacting each'stream of each phase with a separate stream of each other phase in a separate segregated path.

8. A process for treating a mineral oil with a solvent comprising countercurrently contacting said mineral oil and saidsolvent by virtue of a difference in their densities in a plurality of paths of relatively small cross sectional area, said paths containing adsorbent material, and maintaining the proportion of solvent to oil at least substantially the same in each path.

9 .A process for treating a mineral oil with a solvent comprising countercudrently contacting said mineral oil and said solvent by virtue of a difference in their densities in a plurality of paths ofrelativelyrsrnall cross sectional area, said paths containingadsorbent material, maintaining the proportion of solvent to oil at least substantially the same in each path, andreducing the solventr capacity of the solvent in the direction of solvent flow to set up reflux conditions in said paths.

10. A process for treating a mineral oil with a solvent comprising flowing a solution of oil and solvent through a plurality of paths of relatively small cross sectional area, said paths containing adsorbent material, reducing the solvent capacity of the solvent in the direction of solvent flow to throw out of solution mineral oil components of lesser solubility, and choosing the direction of solution flow through said paths so that said precipitated oil components will flow countercurrently to said solution by virtue of a difference in density.

11. A process comprising countercurrently flowing two solvents of incomplete and partial miscibility by virtue of a difierence in their densities through a plurality of paths of relatively small'cross sectional area, said paths containing adsorbent material, and introducing a mineral oil into said paths intermediate the ends thereof.

12. A process for treating a petroleum product with a solvent comprising, countercurrently contacting said petroleum product and said solvent by virtue of a difference in their densities in a column having a plurality of phase contacting paths of relatively small cross sectional area, and maintaining said petroleum product in the form of a slurry with adsorbent material.

. MERRELL R. FENSKE.

WILBERT B. MCCLUER. 

